CN201579045U - Reactor of lifting pipe - Google Patents
Reactor of lifting pipe Download PDFInfo
- Publication number
- CN201579045U CN201579045U CN2009202971989U CN200920297198U CN201579045U CN 201579045 U CN201579045 U CN 201579045U CN 2009202971989 U CN2009202971989 U CN 2009202971989U CN 200920297198 U CN200920297198 U CN 200920297198U CN 201579045 U CN201579045 U CN 201579045U
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- CN
- China
- Prior art keywords
- riser
- pipe
- lifting
- lifting pipe
- nozzle
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model belongs to oil-mixing contact reaction in a catalytic cracking device and provides a reactor of a lifting pipe. A plurality of nozzles (9) are symmetrically distributed on the middle-upper part of the lifting pipe (1); a gas medium pipe (11) used for spraying gas medium to the liquid mist area (12) is arranged above each nozzle; the liquid mist area (12) is arranged in the lifting pipe and above the nozzle outlet; the middle-lower passage (8) of the lifting pipe is a Venturi structure; the bottom part of the lifting pipe is provided with a rectifying pipe (6) and a pre-lifting medium pipe (7); the included angle between the nozzle (9) and the lifting pipe (1) is more than or equal to 35 degrees; one side of the lifting pipe is provided with a regenerating inclined pipe (5); and the regenerating inclined pipe (5) is arranged below the passage (8) with the Venturi structure. The reactor reduces yield of dry gas and coking yield, improves total liquid yield, prevents coking of the lifting pipe and relieves the coking of the catalytic cracking device simultaneously.
Description
Technical field
The utility model belongs to the finish mixing and contacting reaction device in the catalytic cracking unit, relates generally to a kind of riser reactor.
Background technology
Catalytic cracking unit is one of core apparatus of petroleum chemical enterprise, also is China's primary crude oil deep processing device, and working ability surpassed 1.0 hundred million tons/year in 2005, occupied the second in the world.Riser reactor is the nucleus equipment of catalytic cracking unit, and feedstock oil contacts the back and carry out catalytic cracking reaction in riser reactor with catalyst mix.Catalysts influence catalytic cracking reaction speed, the result of itself different chemical reaction and consuming, it is a kind of spheric granules, contacts with industrial wind (or steam) to be transformed into similar flow-like in catalytic cracking unit, circulates in catalytic cracking unit.The catalyst of riser reactor enters the riser reactor bottom from regenerator sloped tube, through wind or steam booster, moves up, and mixes contact at the nozzle place with the feedstock oil through nozzle atomization, carries out catalytic cracking reaction.Generate gasoline, diesel oil, liquid hydrocarbon principal product and accessory substances such as dry gas, coke.Same raw material is at catalytic cracking process, and the key that produces higher total liquid recovery (gasoline, diesel oil, liquid hydrocarbon) is to reduce dry gas yied and coke yield.
Cross section density of catalyst skewness in the riser is " nucleolus structure ", and promptly wall density in limit is big, and center density is little, is mainly caused by the catalyst back-mixing.After nozzle feedstock oil dispersed jet enters riser, above nozzle, form " liquid fog-zone " aggravation catalyst back-mixing.Under nozzle atomization poor performance situation, the big drop of the feedstock oil of generation is run into catalyst and is produced " moist catalysis ", and moist catalysis is to produce riser coking first cause, or the major reason of device coking.Device coking now remains catalytic cracking unit technology trouble first place." crossing cracking " can take place in the Bian Biqu that riser inner catalyst density is big, in the center " thermal cracking " can take place, and crosses cracking and thermal cracking meeting and causes the dry gas coking yield to increase, and total liquid is accepted and fallen.The carrier pipe technology can concentrate on catalyst the center and diffuse to uniform state before nozzle in adopting, but because of interior carrier pipe and riser housing to be open sky to, weaken the catalyst transport capability.
Summary of the invention
The purpose of this utility model is to propose a kind of riser reactor, makes it can reduce dry gas yied and coking yield, improves total liquid and receives, and prevents riser coking and the coking that slows down catalytic cracking unit simultaneously.
For finishing the technical scheme that foregoing invention purpose the utility model adopted be: a kind of riser reactor, comprising that riser, rectification are given promotes section, finish mixed feeding section, finish conversion zone, side at riser is provided with regenerator sloped tube, regenerator sloped tube gives the lifting section with rectification and links to each other, and gives the lifting section in the rectification of riser and is provided with rectifying tube and promotes medium tube in advance; Be provided with several nozzles of symmetrical distribution in the middle and upper part of riser, and be provided with the gas medium pipe that sprays into gas medium to the liquid fog-zone above each nozzle, described liquid fog-zone is positioned at the top of riser, jet expansion; The middle and lower part passage of riser is a Venturi tube structure, and the passage of Venturi tube structure is positioned at rectification and gives the top that promotes section, and the angle between described nozzle and the riser is more than or equal to 35 °.
A kind of riser reactor that the utility model proposes can reduce dry gas yied and coking yield, improves total liquid and receives, the coking that can avoid the riser coking and slow down catalytic cracking unit simultaneously.
Description of drawings
Fig. 1 is a structural representation of the present utility model.
Among the figure: 1, riser, 2, the rectification section of carrying in advance, 3, finish mixed feeding section, 4, the finish conversion zone, 5, regenerator sloped tube, 6, rectifying tube, 7, promote medium tube in advance, 8, the Venturi tube structure passage, 9, nozzle, 11, the gas medium pipe, 12, the liquid fog-zone.
The specific embodiment
With specific embodiment the utility model is illustrated in conjunction with the accompanying drawings:
A kind of riser reactor comprises that riser 1, rectification are given to promote section 2, finish mixed feeding section 3, finish conversion zone 4; Side at riser is provided with regenerator sloped tube 5, and regenerator sloped tube 5 gives lifting section 2 with rectification and links to each other, and gives the lifting section in the rectification of riser and is provided with rectifying tube 6 and promotes medium tube 7 in advance; Be provided with several nozzles 9 of symmetrical distribution in the middle and upper part of riser, and be provided with the gas medium pipe 11 that sprays into gas medium to liquid fog-zone 12 above each nozzle, described liquid fog-zone 12 is positioned at the top of riser, jet expansion; The middle and lower part passage of riser is a Venturi tube structure, and Venturi tube structure passage 8 is positioned at rectification and gives the top that promotes section 2, makes catalyst be higher than admission velocity from the speed of the passage ejection of Venturi tube structure; Obvious reducing appears in the outlet of Venturi tube structure passage, and catalyst cross section density trend evenly; Help contacting, reduce dry gas yied and coking yield, improve total liquid and receive with the mixing of feedstock oil dispersed jet; Slow down " suction function " catalyst back-mixing above nozzle of liquid fog-zone 12, the steam that sprays to liquid fog-zone 12 has further slowed down " suction function "; Prevent the riser coking and slow down the catalytic cracking unit coking; Angle between described nozzle 9 and the riser 1 is more than or equal to 35 °.Among this embodiment, the angle between nozzle 9 and the riser 1 is 35 °.Rectification is given the rectifying tube 6 that promotes the section setting and is promoted medium tube 7 in advance in order to strengthen catalyst fluidization and conveying;
Reactor in use, catalyst enters the rectification pre lift zone 2 of riser reactor bottom through regenerator sloped tube 5, after fluidisation under rectifying tube 6 effects, enters finish compound section 3 through Venturi tube structure passage 8 under the pre-boosting that promotes medium tube 7; Mixing contact good finish limit border ring generation major-minor product and catalyst enters in the catalytic cracking unit settler behind finish conversion zone 4.
Claims (2)
1. riser reactor, it is characterized in that: comprising that riser (1), rectification are given promotes section (2), a finish mixed feeding section (3), finish conversion zone (4), side at riser is provided with regenerator sloped tube (5), regenerator sloped tube (5) gives lifting section (2) with rectification and links to each other, and gives lifting section (2) in the rectification of riser and is provided with rectifying tube (6) and pre-lifting medium tube (7); Be provided with several nozzles (9) of symmetrical distribution in the middle and upper part of riser, and being provided with the gas medium pipe (11) that sprays into gas medium to the liquid fog-zone in the top of each nozzle (9), described liquid fog-zone (12) is positioned at the top of riser, jet expansion; The middle and lower part passage of riser is a Venturi tube structure, and Venturi tube structure passage (8) is positioned at rectification and gives the top that promotes section (2), and the angle between described nozzle (9) and the riser (1) is more than or equal to 35 °.
2. a kind of riser reactor according to claim 1 is characterized in that: the angle between described nozzle (9) and the riser (1) is 35 °.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202971989U CN201579045U (en) | 2009-12-24 | 2009-12-24 | Reactor of lifting pipe |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202971989U CN201579045U (en) | 2009-12-24 | 2009-12-24 | Reactor of lifting pipe |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201579045U true CN201579045U (en) | 2010-09-15 |
Family
ID=42721036
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009202971989U Expired - Lifetime CN201579045U (en) | 2009-12-24 | 2009-12-24 | Reactor of lifting pipe |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201579045U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111748368A (en) * | 2020-07-23 | 2020-10-09 | 洛阳乐邦石化设备有限公司 | Catalytic cracking reactor capable of being flexibly adjusted |
| EP4234079A1 (en) | 2022-02-25 | 2023-08-30 | KMB Catalyst Spolka z o.o. | Aerodynamic multi-phase reactor |
-
2009
- 2009-12-24 CN CN2009202971989U patent/CN201579045U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111748368A (en) * | 2020-07-23 | 2020-10-09 | 洛阳乐邦石化设备有限公司 | Catalytic cracking reactor capable of being flexibly adjusted |
| EP4234079A1 (en) | 2022-02-25 | 2023-08-30 | KMB Catalyst Spolka z o.o. | Aerodynamic multi-phase reactor |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20100915 |